CN103242890A - Method for feeding supplementary catalyst to fluidized catalytic cracking (FCC) device - Google Patents
Method for feeding supplementary catalyst to fluidized catalytic cracking (FCC) device Download PDFInfo
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- CN103242890A CN103242890A CN2012100328888A CN201210032888A CN103242890A CN 103242890 A CN103242890 A CN 103242890A CN 2012100328888 A CN2012100328888 A CN 2012100328888A CN 201210032888 A CN201210032888 A CN 201210032888A CN 103242890 A CN103242890 A CN 103242890A
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Abstract
The invention discloses a method for feeding a supplementary catalyst to a fluidized catalytic cracking (FCC) device. According to the method, a fresh catalyst is fed to a steam stripping section of a settler of the FCC device; a hole is formed in the steam stripping section of the settler of the FCC device, a feeding pipeline is introduced into the steam stripping section of the settler, and a hole is formed in the feeding pipeline behind a vessel wall valve of the feeding pipeline before entering a vessel and is connected with a blowback pipeline and a blowback valve; and a gas source of the blowback pipeline is high-pressure nitrogen gas or dry gas. The method has the advantages that the probability that thermal collapse occurs during fresh catalyst feeding is reduced, the catalyst consumption of the FCC device can be reduced by over 5%, and then, the production cost is lowered.
Description
Technical field
The invention belongs to refining of petroleum industry catalytic cracking process, relate in particular to the method that catalytic cracking process replenished and added catalyzer.
Background technology
Catalytic cracking catalyst is widely used in the FCC apparatus of petrochemical industry, but because a variety of causes, catalyzer usefulness in recycling can reduce gradually, in order to keep the steady of production, all need to replenish in device the live catalyst with the ton metering every day, domestic petrochemical industry is called small-sized reinforced to this operation.Live catalyst is the microsphere particle of normal temperature, in the prior art, the technical process of nearly all FCC apparatus make-up catalyst all is that the method that adopts air to carry is transported to the constant temperature catalyzing agent in the dense-phase bed of FCC apparatus revivifier in the world, and the service temperature of revivifier is generally about 650～750 ℃.
One of reason that catalyst efficiency reduces is that granules of catalyst has produced broken and runs and decrease, because catalytic cracking catalyst is expensive, thereby the broken damage of running can cause bigger loss to the user, and production cost is improved; Catalyst breakage runs the raising that damage can cause dust granules concentration and catalytic slurry solid content in the discharged gas fume on the other hand, and impels the generation of the wearing and tearing of cigarette machine and scale formation, is unfavorable for the smooth running of FCC apparatus.
The reason of catalyst breakage is very complicated.In recent years laboratory study and document show, also can produce fragmentation about 10% at catalyzer in the process of device fresh makeup catalyst, and this situation is called catalyzer heat and collapses.Under the situation that catalyzer makes moist or water content is too high, this situation more so.
Replenish that the reason that heat collapses takes place in the fresh dose of process is that circumstance of temperature difference brings before and after the catalyst transport process thermal shocking and the fresh dose of temperature of injecting the position are higher, but how to solve technical measures that this class catalyzer heat collapses report not almost at present.
Summary of the invention
The technical problem to be solved in the present invention is exactly that broken instant heating when how to reduce the catalytic cracking unit fresh makeup catalyst collapses.The present invention proposes a kind of novel method to the catalytic cracking unit make-up catalyst, can reduce the catalyst consumption of FCC process unit, reduce dust granules concentration and catalytic slurry solid content in the discharged gas fume simultaneously, and can reduce the generation of the wearing and tearing of cigarette machine and scale formation.
For achieving the above object, the technical solution used in the present invention is: rely on catalyzer feeder and charge line in the catalytic cracking unit that prior art possessed, live catalyst is filled into the stripping stage of FCC apparatus settling vessel.
A kind of charging process of catalytic cracking unit make-up catalyst may further comprise the steps:
1) live catalyst in the catalyzer storage tank enters catalyzer feeder and the charge line in the catalytic cracking unit;
2) live catalyst that comes of step 1) mixes with source of the gas in the reverse-blow pipe line before the settling vessel stripping stage;
3) by step 2) live catalyst that comes is filled into the stripping stage of catalytic cracking unit settling vessel.
Because there is high-temperature oil gas in the settling vessel stripping stage, the existing catalyzer feeder of FCC apparatus will be changed into as transmitting power by common pressurized air and adopt high pressure nitrogen or dry gas as transmitting power.The pressurising pipeline source of the gas of the existing catalyst storage tank of FCC apparatus also adopts high pressure nitrogen or dry gas.
By the settling vessel stripping stage position perforate in FCC apparatus, charge line is introduced the settling vessel stripping stage, and perforate on the wall valve back charge line of the charge line before entering the settling vessel stripping stage, connect reverse-blow pipe line and blowback air-valve.The source of the gas of reverse-blow pipe line also adopts high pressure nitrogen or dry gas.
This method no longer directly is filled into live catalyst in the dense-phase bed of FCC apparatus revivifier, but directly is filled into the stripping stage of FCC apparatus settling vessel.Settling vessel stripping stage service temperature is generally 460～500 ℃, live catalyst is entered the environment of 460～500 ℃ of stripping stages in the filling process by the normal temperature state, the instantaneous circumstance of temperature difference of catalyzer changes far below the circumstance of temperature difference that directly is filled into revivifier (650～750 ℃) and changes, reduced the thermal shocking power that instantaneous circumstance of temperature difference changes the live catalyst that brings, the heat that has reduced catalyzer collapses rate.Because the residence time of stripping stage inner catalyst is generally 2～3 minutes, therefore enter fresh dose of stripping stage through with the abundant heat transfer of system's reclaimable catalyst after reach the stripping stage envrionment temperature gradually, then enter revivifier with the stripping stage reclaimable catalyst, this stage, joined circumstance of temperature difference that intrasystem live catalyst runs into and changed forr a short time, the heat that produces collapses also just still less.
Therefore, live catalyst adopts this charging method can reduce the heat that takes place effectively in filling process to collapse.
Implement the present invention and reduced the possibility that generation heat collapses in the filling live catalyst process, can bring following beneficial effect:
(1) agent of FCC apparatus consumption reduces more than 5%, and production cost is reduced.
(2) because in the catalysis flue gas＜minimizing of 20 μ m catalyst fines, therefore can reduce the generation of the wearing and tearing of catalysis cigarette machine and scale formation.
(3) minimizing of catalyst fines can reduce the race damage of FCC apparatus reactive system catalyzer equally, thereby reduces the slurry oil solid content, is conducive to the smooth running of FCC apparatus.
(4) reduce discharging dust in flue gas granule density, reduce surrounding enviroment and pollute.
Implementing the present invention does not need to increase investment renewal feeding equipment, only needs the pipeline of part change conveying catalyzer, and therefore the high pressure nitrogen of consumption or dry gas quantity seldom have the big advantage of the little income of investment.
Description of drawings
Accompanying drawing 1 is the charging technology flow process of prior art;
Accompanying drawing 2 is charging technology flow processs of the present invention.
Reference numeral shown in the figure is: 1-user's catalyzer storage tank, 2-FCC device revivifier, 3-FCC device settling vessel stripping stage, 4-catalyzer feeder, 5-pressurising valve, the 6-charge line, 7-catalyzer feeder is carried air-valve, 8-catalyzer feeder charging valve, 9-catalyzer feeder bleeder valve, 10-wall valve, 11-blowback air valve.
Embodiment
Further specify the present invention below in conjunction with example.
Accompanying drawing one is described as follows.
The charging technology flow process of prior art is the process that the catalyzer that is stored in catalyzer storage tank 1 constantly is transported to FCC apparatus revivifier 2 through feeder 4
User's catalyzer storage tank stores tens of tons of live catalysts usually in the prior art.In order to make catalyzer enter feeder smoothly, need be to the pressurising of catalyzer storage tank, normally 0.1-0.3MPa pressurized air.According to producing needs, manual operation or automated operation catalyzer feeder replenish the live catalyst with the ton metering every day to FCC apparatus revivifier position.This charging process adopts air conveying principle usually, and transmitting power adopts common pressurized air.
Accompanying drawing two is described as follows.
The present invention relies on catalyzer feeder that prior art possessed and charge line (common caliber is DN50) that live catalyst is filled into settling vessel stripping stage in the FCC apparatus.
In the settling vessel stripping stage perforate of FCC apparatus, charge line is introduced the settling vessel stripping stage, and perforate on the wall valve back charge line of the charge line before entering container, connect reverse-blow pipe line and blowback air-valve.
The source of the gas of pressurising pipeline source of the gas, the catalyzer feeder transmitting power of the existing catalyst storage tank of FCC apparatus and the reverse-blow pipe line that installs additional all also adopts high pressure nitrogen or dry gas.
The the present invention of embodiment who is applied to certain commerical test device below in conjunction with accompanying drawing two and the present invention is described in further detail.
The catalyzer storage tank 1 of testing apparatus is designed to pressurized vessel, can store 100 tons of catalyzer.This testing apparatus working ability is 1,000,000 tons/year.According to service data in the past, this device catalyst consumption of 1 ton of raw material of every processing is about 1.1 kilograms, needs about 3 tons of fresh makeup catalyst every day.This installs existing catalyzer feeder 4, can be according to the charge weight of setting operation automatically in batches, to the interior make-up catalyst of device.
Implement the present invention and need transform charge line.Originally small-sized charge line enters the revivifier dense bed, changes to now in this device settling vessel stripping stage perforate, through disengager vessel wall and thermal insulation layer charge line is introduced stripping stage.
Installing two valves additional at charge line, is respectively wall valve and blowback air valve, and model is Z41Y-40R#DN50, is used for cutting off charge line and prevents catalyst reverse flow.Nitrogen, pressure 0.4MPa are adopted in blowback general mood source.Have only blowback air valve 11 to open (air quantity is controlled about 2 cubic metres/hour) and just allow to open wall valve 10.
The existing catalyst storage tank of testing apparatus and catalyzer feeder are not all done change.Catalyzer storage tank pressurising source of the gas changes to 0.3MPa nitrogen by pressurized air, and catalyzer feeder transmitting power changes to 0.6MPa nitrogen.
Implement the present invention 1 year at this device, sum up service data, catalyst consumption is reduced to 0.9 kilogram/ton. and raw material, save catalyst is 200 tons before transforming.
Claims (8)
1. the charging process of a catalytic cracking unit make-up catalyst may further comprise the steps:
1) live catalyst in the catalyzer storage tank enters catalyzer feeder and the charge line in the catalytic cracking unit;
2) live catalyst that comes of step 1) mixes with source of the gas in the reverse-blow pipe line before the settling vessel stripping stage;
3) by step 2) live catalyst that comes is filled into the stripping stage of catalytic cracking unit settling vessel.
2. the charging process of catalytic cracking unit make-up catalyst according to claim 1 is characterized in that: by in described settling vessel stripping stage position perforate, charge line is introduced the settling vessel stripping stage.
3. the charging process of catalytic cracking unit make-up catalyst according to claim 1, it is characterized in that: described reverse-blow pipe line is provided with the blowback air-valve, the reverse-blow pipe line with enter the settling vessel stripping stage before the charge line of wall valve back be connected.
4. the charging process of catalytic cracking unit make-up catalyst according to claim 1, it is characterized in that: described settling vessel stripping stage service temperature is generally 460～500 ℃.
5. the charging process of catalytic cracking unit make-up catalyst according to claim 1, it is characterized in that: the residence time of described catalyzer in stripping stage is 2～3 minutes.
6. the charging process of catalytic cracking unit make-up catalyst according to claim 1 is characterized in that: described catalyzer feeder adopts high pressure nitrogen or dry gas as transmitting power.
7. the charging process of catalytic cracking unit make-up catalyst according to claim 1, it is characterized in that: the pressurising pipeline source of the gas of catalyzer storage tank is high pressure nitrogen or dry gas.
8. the charging process of catalytic cracking unit make-up catalyst according to claim 1 is characterized in that: source of the gas employing high pressure nitrogen or the dry gas of described reverse-blow pipe line.
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| CN201210032888.8A CN103242890B (en) | 2012-02-09 | 2012-02-09 | Method for feeding supplementary catalyst to fluidized catalytic cracking (FCC) device |
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| CN201210032888.8A CN103242890B (en) | 2012-02-09 | 2012-02-09 | Method for feeding supplementary catalyst to fluidized catalytic cracking (FCC) device |
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| CN103242890B CN103242890B (en) | 2015-02-18 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108088792A (en) * | 2017-11-27 | 2018-05-29 | 中国船舶重工集团公司第七二五研究所 | Dirty sample and preparation method and application among a kind of |
| CN109135801A (en) * | 2017-06-16 | 2019-01-04 | 中国石油化工股份有限公司 | Catalyst cracking method and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5944982A (en) * | 1998-10-05 | 1999-08-31 | Uop Llc | Method for high severity cracking |
| CN1695783A (en) * | 2004-05-14 | 2005-11-16 | 中国石油化工股份有限公司 | Method for supplying catalyst / auxiliary agnet for catalytic cracking unit |
| CN101811011A (en) * | 2010-04-13 | 2010-08-25 | 中国石油化工集团公司 | Automatic catalyst-feeding method |
| CN102311758A (en) * | 2010-07-05 | 2012-01-11 | 中国石油化工股份有限公司 | Catalyst injection method and catalyst injection device |
-
2012
- 2012-02-09 CN CN201210032888.8A patent/CN103242890B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5944982A (en) * | 1998-10-05 | 1999-08-31 | Uop Llc | Method for high severity cracking |
| CN1695783A (en) * | 2004-05-14 | 2005-11-16 | 中国石油化工股份有限公司 | Method for supplying catalyst / auxiliary agnet for catalytic cracking unit |
| CN101811011A (en) * | 2010-04-13 | 2010-08-25 | 中国石油化工集团公司 | Automatic catalyst-feeding method |
| CN102311758A (en) * | 2010-07-05 | 2012-01-11 | 中国石油化工股份有限公司 | Catalyst injection method and catalyst injection device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109135801A (en) * | 2017-06-16 | 2019-01-04 | 中国石油化工股份有限公司 | Catalyst cracking method and device |
| CN109135801B (en) * | 2017-06-16 | 2020-11-13 | 中国石油化工股份有限公司 | Catalytic cracking process and apparatus |
| CN108088792A (en) * | 2017-11-27 | 2018-05-29 | 中国船舶重工集团公司第七二五研究所 | Dirty sample and preparation method and application among a kind of |
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